JPH0570454A - Process for producing thiophene - Google Patents

Abstract

Manufacture of thiophene by catalytic dehydrogenation of tetrahydrothiophene. <??>Ruthenium sulphide or a mixture of sulphides of ruthenium and of one or a number of other transition metals is employed as a bulk or supported catalyst.

Description

Detailed Description of the Invention

The present invention relates to the production of thiophene by catalytic dehydrogenation of tetrahydrothiophene.

Thiophene is widely used as an intermediate for the synthesis of pharmaceuticals (antihistamines, platelet coagulants, cephalosporins, anti-inflammatory agents, etc.), stabilizers for polymers and colorants (diazothiophene), and its use is rapid. Is expanding to.

There are many methods for producing thiophene, and the starting materials are different as follows.

-1-butene or butadiene and CS ₂ (F
R patent 2,139,177), butane or 1-butene, H ₂ S and sulfur (FR patent 2,2)
42,391 No.), - butanediol and vaporized sulfur (BE Patent 671,591),-n-butanol or 1,4-butanediol and CS ₂
(FR Patent No. 2,139,177), - crotonaldehyde and H ₂ S (FR Patent 2,375,227
No.) - Although furan and H ₂ S (BE Patent 623,801) the end of the process is industrially to, furan not must be supplied at low cost, not Sokusa circumstances in many countries. Other processes suffer from selectivity problems due to the formation of many undesired products and require frequent regeneration due to the catalytic processes that result in rapid catalyst coking.

A particularly attractive starting material for the production of thiophene is tetrahydrothiophene (hereinafter abbreviated as THT), which is industrially synthesized from tetrahydrofuran, which is a low cost raw material. The plant for the production of thiophene is advantageously arranged subsequent to the industrial synthesis of THT from tetrahydrofuran, without investing too much capital. Furthermore, THT can be easily separated from thiophene, thus eliminating the need to work at total conversion and adapting the production of industrial units to the requirements.

Several studies have been done on the dehydrogenation of THT. It is known to use aluminum oxide and cobalt oxide, or aluminum oxide, cobalt oxide and molybdenum oxide as the catalyst for this reaction (R.
D. Obolentsev, Khim. Seroorgan. Soedin. Soderzhasc
h, v. Nelft. 1 Nefteprod. Akad. Nauk USSR, Bashkir
sk.Filia l 4, 245-255,1961 and Bashkirsk.Filial 7 ,
148-155, 1964), a good yield is obtained in the early stage of the reaction, but the good yield is not sustained. The activity of the catalyst drops very quickly. This is because the dehydrogenation reaction is blocked by coking.

The oxidative dehydrogenation of THT with SO _{2 in} the presence of a catalyst (metal oxide, activated alumina or activated carbon) is described in FR patent 2,071,189. The patent shows that the best results are obtained at 500-600 ° C, that if the temperature is too low, the catalyst deactivates significantly, mainly due to the condensation of sulfur, and that the decoking is incomplete. There is.

A paper entitled "Study on Mechanism of Thiophene Formation in the Presence of Sulfide Catalysts" (Geterog. Katal, 1979,
4th Pt. 2, 237-42; Chemical Abstracts, 93, 13
1779d), TS Sukhareva et al. Teach that the most active catalysts are rhenium, molybdenum, iron and platinum sulfides.

The present inventors have found that ruthenium sulfide has very high activity in dehydrogenation of THT and has high selectivity. The use of ruthenium sulphide-based catalysts allows dehydrogenation to be carried out at relatively low temperatures and stabilizes the activity of the catalyst for long periods of time.

The subject of the invention is therefore a process for the production of thiophenes by catalytic dehydrogenation of THT, characterized in that a stream of THT is passed over a catalyst based on ruthenium sulfide.

Ruthenium sulfide is lumpy and very active. However, for convenience of use on an industrial scale, ruthenium sulfide is a supported type which may have a ruthenium content of from 2 to 60% by weight, preferably from 2 to 20% by weight, particularly preferably from 5 to 15% by weight. It is preferably used in the form of a catalyst. The support can be, for example, alumina, silica, diatomaceous earth, titanium oxide, zirconium oxide, silica-alumina, thorium oxide or activated carbon.

Ruthenium sulfide and sulfides of at least one transition metal selected from the group consisting of vanadium, chromium, molybdenum, rhodium, palladium, tungsten, manganese, niobium, nickel, iron or cobalt. Of a metal other than Ru in the mixture can be up to 80 atom%.
Are also included in the scope of the present invention.

The sulfide, whether or not supported, can be produced by various known methods such as the following.

Bulk catalyst: sodium sulfide is added to a solution of at least one metal chloride in methanol for precipitation, followed by extraction of sodium chloride and finally hydrogen and H _2.
The solid is treated in the presence of a mixture of S (2-50% by volume, preferably 15%) at a temperature of 300-600 ° C, preferably about 400 ° C.

Supported catalyst: the support is impregnated with one or more metal salts, for example chloride, followed by 300 to 700 ° C.
Hydrogen and H ₂ S (2 to 50% by volume, preferably about 15% by volume) at a temperature of preferably 400 to 600 ° C, more preferably about 500 ° C.
%) Or by direct sulfurization with H ₂ S diluted in an inert gas (eg nitrogen).

The high temperature treatment with a mixture of H ₂ S + diluent (hydrogen or an inert gas) preferably comprises reacting the catalyst for the production of thiophene with the catalyst in a suitable form, for example tablets obtained by methods known per se. After placing in form, it is carried out in the reactor.

As long as the conditions for carrying out the dehydrogenation reaction of THT are such that the temperature does not limit the shift of the thermodynamic equilibrium toward the complete formation of thiophene and the partial pressure of THT and H ₂ S, a high yield is obtained. Can be varied over a wide range without hindering obtaining thiophene. Operation is 300 to 600 ℃
It may be carried out at a temperature of between 350 to 450 ° C, more preferably about 380 to 420 ° C. Reaction is atmospheric pressure or
It can be carried out at high pressures up to 15 bar (absolute pressure). The contact time can vary between 0.1 and 10 seconds, but is preferably between 1 and
3 seconds.

For example, an inert diluent such as a noble gas or nitrogen can be used to limit the partial pressure of THT in the air stream over the catalyst. However, H ₂ S
/ THT molar ratio in the range of 0.1 to 10, preferably 1 to
It is preferred to dilute THT with H ₂ S, as 5, especially about 4.

[0019]

The present invention is illustrated by the following examples, which do not limit the present invention.

Example 1 Unsupported transition metal sulfides were prepared using the operating procedure described in the literature (J. Catal, 120, 473, 1989).

The sulfide thus synthesized was tested in the dehydrogenation reaction of tetrahydrothiophene under the following conditions.

Temperature 380 ° C. Total pressure 1 bar THT partial pressure 6.6 × 10 ² Pa H ₂ S partial pressure 6.6 × 10 ² Pa Using a tubular glass microreactor with a volume of 30 ml, 50
Continuous operation with ~ 300 mg of catalyst mass. The total flow rate was generally 60 ml. Saturator-conde by keeping THT in a closed reactor at a constant temperature
nser) and the partial pressure of THT was determined by its temperature. The gas effluent leaving the reactor was analyzed using gas phase chromatography.

Table 1 shows the catalytic activity measured in the quasi-steady state.

The activity of the ruthenium sulfide of the present invention is far superior to that of the other metal sulfides tested.

[0025]

[Table 1]

Example 2 Three alumina-supported catalysts were prepared by impregnating transitional alumina with various salt precursors of vanadium sulfide, molybdenum sulfide or ruthenium sulfide. For vanadine and molybdenum based catalysts, ammonium thiovanadate and ammonium heptamolybdate were used, respectively. In the case of ruthenium-based catalysts, ruthenium chloride was used to better disperse the ruthenium and to make it more sulphidic.

The alumina used was cubic γ-alumina and was preformed into 1.2 mm extrudates. Its specific surface area is 232 m ² / g and this support has a pore volume of 0.64 cm ³ / g. The loss on ignition at 1,000 ° C is 2.1%.

The support is pre-dried at a temperature between 100 and 250 ° C., preferably 180 ° C. and brought into contact with an aqueous solution of the metal salt corresponding to the desired catalyst. The amount of water used is equal to the pore volume of the carrier, but in some cases up to 3 times the excess water required to fill the pores of the carrier may be used.

After being dried at 100 to 200 ° C., the precursor material was converted to H 2
Sulfurized by treatment with a mixture of ₂ S and nitrogen (for Ru) or hydrogen (for Mo and V) at 400 ° C. for 4 hours. The H ₂ S content is approximately 15% by volume.

The supported catalyst thus obtained was then tested in the THT dehydrogenation reaction under the same conditions as in Example 1.
The results obtained are shown in Table 2. In the table, the second column shows the content weight of the metal (Mo, V or Ru) of the carrier catalyst.

[0031]

[Table 2]

These results show that even when ruthenium sulfide is dispersed on a carrier such as alumina, the remarkably good dehydrogenation properties obtained with non-supported ruthenium sulfide are retained.

Example 3 The effect of the activation conditions of the Ru / Al ₂ O ₃ catalyst (Ru 7% by weight) was investigated by proceeding with a catalytic test under the same operating conditions used in the previous example. Table 3 shows the activity and selectivity obtained with the N ₂ / H ₂ S mixture (H ₂ S 15% by volume) for different activation temperatures of the catalyst.

[0034]

[Table 3]

[0035]Example 4  The results shown in Examples 1 and 2 are the same for the supported type.
Not even RuS₂Showing the superiority of pyrite-type phases
It Therefore, RuS containing 7 wt% Ru₂/ Al
₂O₃The catalyst was operated under the following operating conditions on a micropilot scale.
Tested.

THT flow rate: 0.33 mol / hr H ₂ S flow rate: Fluctuation Catalyst amount: 38 g Reaction temperature: 380 ° C. Total pressure: 1 bar Addition of H ₂ S results in production of hydrocarbons by cleavage of C—S bond Side reactions are limited and the reactants are diluted to increase the critical conversion added by thermodynamics. Furthermore, the presence of hydrogen sulphide allows the catalyst to be retained in the sulphided form.

The reactor used is 316 with a length of 800 mm and a diameter of 25 mm.
A fixed bed reactor comprising vertical stainless steel tubes,
A temperature-measuring exterior is installed to allow precise adjustment of the temperature curve along the catalyst bed. THT is introduced in liquid form using a pump and is contacted with H ₂ S in a preheater placed upstream of the reactor and maintained at 150 ° C so that THT can be rapidly volatilized. The liquid phase is collected in a condenser as it exits the reactor.

H ₂ S / TH for the selectivity of thiophene
The effect of the T molar ratio was investigated under operating conditions which resulted in a total conversion of the order of 30%. The results obtained are shown in Table 4.

[0039]

[Table 4]

Example 5 The action of the RuS ₂ / Al ₂ O ₃ catalyst over time was changed to H ₂ S
The / THT ratio was set to 2 and examined under the same operating conditions as in the previous example. Table 5 shows the changes in the conversion rate and the selectivity for thiophene with the passage of time of use of the catalyst.

[0041]

[Table 5]

These results show that the catalyst deactivates linearly with the lapse of time and no change in selectivity is observed. Under the operating conditions used, the half-life of the solid is approximately 200 hours.

Example 6 The catalyst of the previous example contained approximately 17% by weight of "coke".
Contains. To remove this, the spent catalyst is regenerated with air or a mixture of air and water (air / water molar ratio = 20). This oxidation treatment is contacted with catalyst-air (or air + water) at 350 ° C. for about 3 seconds.

After this treatment, the sulfide phase converted into oxide or oxosulfide was treated with H ₂ S under the same conditions as in Example 2.
Sulfide by treatment with a / N ₂ mixture.

The results obtained with the regenerated catalyst are shown in Table 6.

[0046]

[Table 6]

Generally, the regeneration process is carried out between 300 and 600 ° C.
It can be carried out preferably at a temperature of 350 to 400 ° C. and a contact time of 0.1 to 10 seconds. If an air + water mixture is used, the air / water molar ratio can range from 1-40.

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Kristian Foulkey United States, Pennsylvania 19333, Devan, Brytan Circle 603 (72) Inventor Michel Lacroix France, 69009 Lyon, Cyumann-Dou Mont-Uribreble , 27. Se (72) Inventor Missier Bruise France, 69300, Callilleil and Quiille, Lieux Pierre Bourjois, 15

Claims (9)

[Claims] 1. A method for producing thiophene by catalytic dehydrogenation of tetrahydrothiophene, which comprises passing a stream of tetrahydrothiophene over a catalyst based on ruthenium sulfide. 2. The method according to claim 1, wherein ruthenium sulfide is used in bulk. 3. Ruthenium sulfide is deposited on the carrier,
The method of claim 1. 4. The carrier is alumina, silica, diatomaceous earth,
The method according to claim 3, which is titanium oxide, zirconium oxide, silica-alumina, thorium oxide or activated carbon. 5. The ruthenium content of the supported catalyst is from 2 to 60.
% By weight, preferably 2 to 20% by weight, more preferably 5
The method according to claim 3 or 4, which is -15% by weight. 6. Dehydrogenation is performed at 300 to 600 ° C., preferably 350.
6. The method according to any one of claims 1-5, which is carried out at a temperature of ~ 450 ° C, more preferably about 380-420 ° C. 7. The reaction is atmospheric pressure or 15 bar (absolute pressure)
7. The method according to any one of claims 1-6, which is carried out at a pressure of 8. Tetrahydrothiophene using an inert gas, or preferably 0.1-10, preferably 1-5,
It is diluted in particular with hydrogen sulfide in a molar ratio of about 4 H ₂ S / tetrahydrothiophene A method according to any one of claims 1 to 7. 9. Ruthenium sulfide, vanadine, chromium,
A mixture with a sulfide of at least one transition metal selected from the group consisting of molybdenum, rhodium, palladium, tungsten, manganese, niobium, nickel, iron and cobalt is used, the proportion of metals other than ruthenium in the mixture being 9. The method according to any one of claims 1-8, which is up to 80 atom%.